Para-xylene-separation with aluminosilicate X-type zeolite compositions with low LTA-type zeolite

ABSTRACT

A process for separating para-xylene from a mixture of C 8  alkylaromatics comprises contacting the mixture of C 8  alkylaromatics with a zeolitic binder-converted composition comprising (a) a zeolite X composition having at least a first zeolite X having a mean diameter not greater than 2.7 microns, and a second zeolite X, wherein the second zeolite X is obtained by converting a binder material to the second zeolite X and the binder material is in a range from 5 to 50 wt % of the zeolite X composition; and (b) an unconverted binder material content, after conversion to the second zeolite X is complete, in a range from 0 to 3 wt % of the zeolite X composition. The zeolite X composition has an average Si/Al framework mole ratio in a range from 1.0 to 1.5, and a relative LTA intensity not greater than 1.0, as determined by x-ray diffraction (XRD).

CROSS-REFERENCE TO RELATED APPLICATION

This application claims benefit of U.S. Provisional Application No.61/474,923 filed on Apr. 13, 2011.

FIELD OF THE INVENTION

This invention relates a process for separating para-xylene from otherC₈ alkylaromatics using a new binder-converted composition derived froma new family of X-type aluminosilicate zeolites. More specifically, thisnew binder-converted composition is made using X-type zeolites havingeither low or no detectable levels of LTA-type zeolite, as determined byx-ray diffraction, and binder material convertible to X-type zeolite.

BACKGROUND OF THE INVENTION

Zeolites are crystalline aluminosilicate compositions that aremicroporous and that are formed from corner sharing AlO₂ and SiO₂tetrahedra. Numerous zeolites, both naturally occurring andsynthetically prepared are used in various industrial processes.Synthetic zeolites are prepared via hydrothermal synthesis employingsuitable sources of Si, Al and structure directing agents such as alkalimetals, alkaline earth metals, amines, or organoammonium cations. Thestructure directing agents reside in the pores of the zeolite and arelargely responsible for the particular structure that is ultimatelyformed. These species balance the framework charge associated withaluminum and can also serve as space fillers. Zeolites are characterizedby having pore openings of uniform dimensions, having a significant ionexchange capacity, and their ability to adsorb and reversibly desorb anadsorbed phase that is dispersed throughout the internal voids of thecrystal without significantly displacing any atoms that make up thepermanent zeolite crystal structure.

Among other uses, zeolites can be used to make an adsorbent material. Inadsorbent materials, zeolites can separate components of eithermulti-component gas mixtures or liquid mixtures. It's generallyunderstood that the presence of an inert or non-reactive zeolite(“contaminant zeolite”) can often diminish the adsorption performance ofcertain zeolites. Conventionally, however, the presence of somerelatively low, but still tolerable, concentration of a contaminantzeolite has been viewed as commercially acceptable since it's generallyconsidered to produce an insignificant loss or drop in the finishedadsorbent's performance. Accordingly, there's a diminishing point ofreturn in further reducing contaminant zeolite levels. Soconventionally, it's been considered more cost-effective to leavecontaminant zeolite(s) mixed with the active zeolite, than to remove orfurther reduce the contaminant zeolite in light of its relatedadsorbent's projected performance.

Accordingly, there is a need for a zeolite with improved purity, moreparticularly an X type zeolite that can have a more beneficial effect onthe zeolite's process performance than expected for the extent to whichthe contaminant zeolite content is either further reduced, beyondcustomary levels, or fully removed.

Despite this conventional view, however, Applicants have discovered andsuccessfully made a zeolite with little to no detectable amounts of aparticular contaminant zeolite, namely, a LTA-type zeolite (hereinafter“LTA zeolite”). More specifically, Applicants have discovered and made aform of zeolite X with either little or no detectable LTA zeolite (“lowLTA-containing X zeolite”), as determined by the x-ray diffraction(“XRD”) method described below, which also has a particle size notgreater than 2.7 microns (μm), as determined by the sedigraph analysisdescribed below. Applicants have also discovered that a lowLTA-containing X zeolite is useful for making a zeoliticbinder-converted composition (discussed below).

One adsorbent application of interest, among others, relates toseparating para-xylene (pX) from a mixture of xylenes in a fixed bedprocess, which is often a simulated moving bed (SMB) adsorption process.

The SMB adsorption process is used commercially in a number of largescale petrochemical separations to recover high purity pX from mixedxylenes. As used herein, “mixed xylenes” refers to a mixture of C₈aromatic isomers that includes ethyl benzene (EB), pX, meta-xylene (mX)and ortho-xylene (oX). High purity pX is used for the production ofpolyester fibers, resins and films. Typically, pX is converted toterephthalic acid (TPA) or dimethyl terephthalate (DMT), which is thenreacted with ethylene glycol to form polyethylene terephthalate (PET),the raw material for most polyesters.

The general technique employed in the performance of SMB adsorptiveseparation processes is widely described and practiced. Generally, theprocess simulates a moving bed of adsorbent with continuouscounter-current flow of a liquid feed over the adsorbent. Feed andproducts enter and leave adsorbent beds continuously, at nearly constantcompositions. Separation is accomplished by exploiting the differencesin affinity of the adsorbent for pX relative to the other C₈ aromaticisomers.

Typical adsorbents used in SMB adsorption processes generally includecrystalline aluminosilicate zeolites and can comprise both the naturaland synthetic aluminosilicates. Suitable crystalline aluminosilicatezeolites for use as an adsorbent selective for pX include those havingaluminosilicate cage structures in which alumina and silica tetrahedraare intimately connected with each other in an open three dimensionalcrystalline network. The tetrahedra are cross linked by shared oxygenatoms, with spaces between the tetrahedra occupied by water moleculesprior to partial or total dehydration of the zeolite. The dehydrationresults in crystals interlaced with channels having moleculardimensions.

In a hydrated form the crystalline aluminosilicate zeolites aregenerally represented by the formula:M_(2/n)O:Al₂O₃:wSiO₂:yH₂Owhere “M” is a cation that balances the electrovalence of the tetrahedraand is generally referred to as an exchangeable cationic site, “n”represents the valence of the cation, “w” represents the moles of SiO₂,and “y” represents the moles of water. Such crystalline aluminosilicatezeolites that find use as an adsorbent possess relatively well-definedpore structures. The exact type aluminosilicate zeolite is generallyidentified by the particular silica: alumina molar ratio and the poredimensions of the cage structures.

Cations (M) occupying exchangeable cationic sites in the zeoliticadsorbent may be replaced with other cations by ion exchange methodswell known to those having ordinary skill in the field of crystallinealuminosilicates. Crystalline aluminosilicates, such as zeolite X withbarium and potassium cations at the exchangeable cationic sites withinthe zeolite, are known to selectively adsorb pX in a mixture comprisingat least one other C₈ aromatic isomer beyond pX.

Generally, zeolitic adsorbents used in separation processes contain thezeolitic crystalline material dispersed in an amorphous material orinorganic matrix having channels and cavities that enable liquid accessto the crystalline material. Silica, alumina or certain clays andmixtures thereof are typical of such inorganic matrix materials, whichact as a “binder” to form or agglomerate the zeolitic crystallineparticles that otherwise would comprise a fine powder. Agglomeratedzeolitic adsorbents may thus be in the form of extrudates, aggregates,tablets, macrospheres such as beads, granules, or the like.

The binder is typically inert and contributes little, if any, to theadsorptive separation process. Efforts to improve adsorbent efficacygenerally have focused on (a) decreasing the size of the zeoliteparticles forming the adsorbent and (b) increasing the zeolite volume(i.e., the active separation component) within adsorbents. One methodfor increasing the zeolite volume in the adsorbent is to convert thebinder into zeolite in a conversion process referred to as“zeolitization,” while preferably maintaining or improving the adsorbentmaterial's strength and macroporosity, among other things. Thisbinder-conversion process thereby obtains a zeolitic binder-convertedcomposition, which is often referred to as a “binderless” zeoliticadsorbent. However, the description of “binderless” does not necessarilymean all original binder material is converted to zeolitic materialsince some small fraction of binder material (e.g., up to 3 wt %) maynot be converted, depending on various factors, such as, original bindercontent, zeolitization conditions, etc. While a binder-conversionprocess has resulted in improved adsorbent efficacy, still furtherimprovements in adsorptive separation process efficiency are desired.

Accordingly, an improved zeolitic binder-converted adsorbent compositionobtained from a X zeolite with improved purity—more specifically, a lowLTA-containing X zeolite having a particle size not greater than 2.7μm—to recover high purity pX from mixed xylenes in a liquid-phaseseparation process using the zeolitic binder-converted adsorbent isdescribed more fully herein. A method for obtaining a low LTA-containingX zeolite having a particle size not greater than 2.7 μm is alsodescribed herein, as well as a method for obtaining a zeoliticbinder-converted adsorbent using such a low LTA-containing X.

Furthermore, other desirable features and characteristics of the presentinvention will become apparent from the subsequent detailed descriptionof the invention and the appended claims.

SUMMARY OF THE INVENTION

According to one aspect of the invention, there is provided a processfor the separation of para-xylene from a mixture of C8 alkylaromatics,comprising contacting the mixture of C8 alkylaromatics with a zeoliticbinder-converted composition under adsorption conditions, the zeoliticbinder-converted composition comprising: (a) a zeolite X compositionhaving at least a first zeolite X having a mean diameter not greaterthan 2.7 microns, as determined by sedigraph analysis, and a secondzeolite X, wherein the second zeolite X is obtained by converting abinder material to the second zeolite X and the binder material is in arange from 5 to 30 wt % of the zeolite X composition, and (b) anunconverted binder material content, after conversion to the secondzeolite X is complete, in a range from 0 to 3 wt % of the zeolite Xcomposition; wherein the zeolite X composition has

-   (i) an average Si/Al framework mole ratio in a range from 1.0 to    1.5, wherein the Si/Al framework mole ratio of the first zeolite and    the second zeolite may be the same or different; and-   (ii) a relative LTA intensity not greater than 1.0, as determined by    a x-ray diffraction (XRD) method using a source of CuKα radiation to    obtain XRD intensities in range from 5° to 25° 2θ,    wherein, the relative LTA intensity is calculated as 100 times the    quotient of

$\frac{a\mspace{14mu}{sample}\mspace{14mu}{LTA}\mspace{14mu}{XRD}\mspace{20mu}{intensity}\mspace{20mu}{for}\mspace{20mu}{the}\mspace{20mu}{zeolite}\mspace{20mu} X}{\begin{matrix}{a\mspace{20mu}{reference}\mspace{20mu}{XRD}\mspace{20mu}{intensity}\mspace{25mu}{for}\mspace{20mu} a\mspace{20mu}{LTA}\mspace{20mu}{zeolite}} \\{{reference}\mspace{20mu}{material}\mspace{20mu}{consisting}\mspace{20mu}{essentially}\mspace{20mu}{of}\mspace{20mu}{LTA}\mspace{20mu}{zeolite}}\end{matrix}}$wherein,

-   (1) the sample LTA XRD intensity of the zeolite X composition is the    sum of the intensities for each LTA peak with Miller indices of (2 0    0), (4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50°    2θ, and-   (2) the reference XRD intensity of the LTA-type zeolite reference    material is the sum of the intensities for each LTA peak with Miller    indices of (2 0 0), (4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34°    and 24.27±0.50° 2θ,    -   wherein,    -   the sample LTA XRD intensity and the reference XRD intensity are        each-   (a) obtained for a sodium-exchanged form of the zeolite X    composition and the LTA-type zeolite reference material,    respectively, and-   (b) equilibrated at 50% relative humidity.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows 3 XRD scans providing three LTA zeolite peaks with theirrespective Miller indices and 2θ values, which can be used fordetermining the LTA zeolite content of different sample materials,wherein scan A is a XRD scan of a reference material, a Na-exchangedzeolite A; scan B is an XRD scan of a comparative material, prepared inaccordance with the synthesis example (C-1) but fully Na-exchanged priorto XRD analysis, and scan C is an XRD scan of a low-LTA containing Xzeolite indicating no detectable LTA zeolite, also fully Na-exchangedprior to XRD analysis.

FIG. 2 illustrates the same comparative scans of FIG. 1, but with theNa-exchanged zeolite A reference scan not shown and at 10× magnificationso the three LTA zeolite peaks best indicating the presence of LTAzeolite, if any, are more easily observed.

DETAILED DESCRIPTION OF THE INVENTION

Applicants have prepared a zeolitic binder-converted compositionproduced with a zeolite having a low or no detectable LTA zeolite havingimproved performance for the separation of para-xylene from a mixture ofother C₈ alkylaromatic hydrocarbons.

Zeolite X Preparation

The structure of zeolite X is described in detail in U.S. Pat. No.2,882,244. A low LTA-containing X zeolite, as determined by the XRDmethod described below, having a particle size not greater than 2.7 μm,as determined by the sedigraph analysis described below, can beprepared, for example, using either a zeolite seed material or initiatormaterial. Zeolite particle size is sometimes referred to in the art ascrystallite size, but for consistency particle size will be used herein.

Smaller zeolite particle sizes can be obtained using a seed or initiatormaterial for initiating zeolite crystallite growth (sometimes describedas nucleation). So a seed or initiator material is first prepared andthen blended into a gel composition at a gel composition to initiatorratio to obtain a zeolite particle size in a targeted range. The ratioof gel composition to seed or initiator material governs the relativenumber or concentration of nucleation sites, which in turn affects theparticle size obtained for the zeolite X. Generally, higherconcentrations of seed or initiator material reduce the particle size.For example, zeolite X preparations having mean diameter in a range from2.7 microns to 0.5 microns can be made using gel to seed/initiatorratios in a range from 7900 to 1 and 85 to 1, by weight, respectively.In view of the present disclosure, those having skill in the art canreadily vary the gel to seed or initiator weight ratios to obtain anyaverage zeolite particle size not greater than 2.7 μm.

A typical gel composition comprises Na₂O, SiO₂, Al₂O₃, and water. TheApplicants have found that, generally, as the amount of Na₂O usedrelative to the other gel or initiator components (i.e., SiO₂, Al₂O₃,H₂O) is increased, the mean diameter of the zeolite X obtained isreduced. However, as the amount of Na₂O in the gel or initiatorcomposition increases, there is an increased tendency to producecontaminant LTA zeolite. Also, when an increased concentration of Na₂Ois used relative to SiO₂ and Al₂O₃, the ratio of SiO₂ to Al₂O₃ iseffectively reduced, which in turn obtains a lower Si/Al framework ratioin the zeolite when a seed or initiator material is used to make the Xzeolite. But generally, a lower Si/Al framework ratio results in alarger zeolite framework unit cell size (UCS), which in turn canadversely affect the zeolite's selectivity for certain species ofinterest. Accordingly, while obtaining smaller particle size byincreasing the Na₂O concentration can be beneficial, at the same time itcan create other undesired attributes, such as formation of contaminantLTA zeolite and a larger UCS.

Interestingly, if an initiator or seed material is not used to make thezeolite X, the smallest obtainable mean diameter is 3 μm, even when thetotal Na₂O, SiO₂ and Al₂O₃ molar ratios are substantially the same orsimilar to those for a synthesis using an initiator or seed material.

Applicants have surprisingly discovered how to produce a Zeolite X withdecreased UCS, while producing little to no detectable LTA zeolite inthe formation of Zeolite X. Total mole ratios for primary reactantsrelative to Al₂O₃, including seed or initiator material contributions,for a small particle, low LTA-containing X zeolite are provided below.

Small Particle, Low LTA-containing X Zeolite with Initiator Range Na₂OSiO₂ Al₂O₃ H₂O Broad 3.94-4.05 2.96-3.34 1.00 200.1-202.8 Preferred3.99-4.02 3.15-3.24 1.00 201.5-202.1 Example S-1 & S-2 4.02 3.24 1.00202.1

For comparative purposes, the typical mole ratios for a conventionalsmall particle, high LTA-containing X zeolite synthesis for primaryreactants relative to Al₂O₃, including seed or initiator materialcontributions are provided below.

Small Particle, High LTA-containing X Zeolite with Initiator Range Na₂OSiO₂ Al₂O₃ H₂O Broad 3.86-3.93 2.70-2.95 1.00 198.3-200.1 Example C-13.93 2.95 1.00 200.1

For comparative purposes, the typical mole ratios for a conventionallarge particle (i.e., >3 μm mean diameter), low LTA-containing X zeolitesynthesis without initiator for primary reactants relative to Al₂O₃ areprovided below.

Large Particle, Low LTA- containing X Zeolite without Initiator RangeNa₂O SiO₂ Al₂O₃ H₂O Broad 2.50-4.26 2.77-3.01 1.00 65-240 Example C-22.63 2.83 1.00 79.9

As noted above, the smallest mean diameter obtainable for an X zeolitemade without an initiator or seed material is 3 μm. And although such alarge particle zeolite X tends to have a low LTA content, it cannotobtain a mean diameter below 3 μm without an initiator or seed material,which inevitably leads to producing an undesirably high LTA content,absent Applicant's newly discovered process for making a lowLTA-containing X zeolite with a mean diameter not greater than 2.7 μm.

Gel Composition

A gel composition may be prepared by combining a gel makeup solutionwith an aluminate makeup solution containing, for example, about 12%alumina by weight. The gel makeup solution is prepared by mixing water,caustic solution, and sodium silicate, and cooling the mixture to about38° C. (100° F.). The aluminate makeup solution is prepared bydissolving alumina trihydrate in a caustic solution, with heating asnecessary for dissolution, followed by cooling and aging at about 38° C.(100° F.) prior to combining it with the gel makeup solution. The gelmakeup solution and aluminate solution are then combined under vigorousagitation for a short period (e.g., about 30 minutes), prior to addingthe required amount of seed.

Seed Material Preparation

The seed is prepared in a similar manner to the gel composition. Atypical seed composition therefore also comprises Na₂O, SiO₂, Al₂O₃, andwater. For each mole of Al₂O₃, about 10-20 moles of Na₂O and SiO₂, andabout 150-500 moles of water, can be used. The aluminate solution usedin preparing the seed may contain, for example, about 18% alumina byweight. After the gel composition and seed are combined, the mixture isheated while agitation is maintained, and then aged under agitatedconditions for a time from about 5 to about 50 hours and at atemperature from about 25° C. (75° F.) to about 150° C. (300° F.) toachieve the desired crystallite formation from the seed nuclei. Theresulting solid material can then be filtered, washed, and dried toobtain a small particle size zeolite X. The particle size of the zeoliteX is determined by the sedigraph analysis, as described more fully underthe characterization examples section below.

Binder

Zeolite X is used in the synthesis of a binder-converted composition bycombining the first “prepared” or already made zeolite X with a zeoliteX-precursor. The preferred zeolite X-precursors include clays that willobtain a Si/Al framework ratio in a range from 1 to 1.5 and preferably,a Si/Al framework ratio substantially consistent with the preferredSi/Al ratio in a range from 1.15 to 1.35 for the original lowLTA-containing X zeolite before clay conversion. More preferably, thezeolite X-precursors are clays such as kaolin, kaolinites, andhalloysite. The zeolite X-precursors are used to make a second zeolite Xin a binder-converted composition.

Preferably, the mean particle diameter of the binder material is in arange from 0.4 to 4.6 μm.

The forming procedure involves combining the zeolite X-precursor,exemplified by kaolin clay, with the zeolite X powder of the preparedfirst zeolite X and optionally other additives such as pore-generatingmaterials (e.g., corn starch to provide macroporosity) and water asneeded to obtain the proper consistency for shaping. Shaping or forminginto larger beads, spheres, pellets, etc., can be performed usingconventional methods including bead forming processes such as Nautamixing, tumbling, or drum rolling to prepare larger particles (e.g., inthe range of about 16-60 Standard U.S. Mesh size). The formed particlescomprising the prepared first zeolite X and the zeolite X-precursor arethen activated at a temperature generally ranging from about 500° C. toabout 700° C. (about 930° F. to about 1300° F.). In the case of azeolite X-precursor comprising kaolin clay, activation causes thismaterial to undergo endothermic dehydroxylation, whereby the disordered,meta-kaolin phase is formed.

Following activation, caustic digestion of the formed particles (e.g.,using sodium hydroxide), then converts the activated zeolite X-precursorinto a second zeolite X, resulting in a binder-converted compositionthat may comprise or consist essentially of zeolite X, with low or nodetectable LTA zeolite content.

The Si/Al framework ratio of the converted portion of zeolite X, as wellas the contribution of this material in the final formulation, may bevaried according to the type and amount of zeolite X-precursor that isincorporated into the formed particles. Normally, the Si/Al ratio of thezeolite X-precursor will be substantially conserved upon conversion intozeolite X. Thus, a typical kaolin clay having a Si/Al ratio in a rangefrom 1.0 to 1.1 will convert to a zeolite X portion having a zeoliteframework ratio within this range. It is possible, therefore, to preparebinder-converted compositions having first (prepared) and second(converted) portions of zeolite X with differing Si/Al ratios.

However, increasing the Si/Al framework ratio of zeolite X, from a rangeof 1.0 to 1.1 to a range from 1.05 to 1.35, can result in increaseddesorbent strength (e.g., with para-diethylbenzene (pDEB) desorbent) inthe adsorptive separation of pX. When zeolite X having a Si/Al frameworkratio of 1.0 is substituted for higher ratio zeolite X in the adsorbentformulation, the pDEB desorbent strength is reduced considerably (i.e.,the value of the inverse of the relative desorbent strength increases).This reduction in desorbent strength, which affects the ability of thedesorbent to displace the desired pX product into an extract stream, canhave adverse consequences in terms of obtaining pX with a high purityand recovery, particularly in a commercial process for the adsorptiveseparation of pX operating in a simulated moving bed mode.

These results illustrate the process efficiencies that can be gainedfrom the use of binder-converted compositions in which the convertedportion of zeolite X has a Si/Al framework ratio in the range from 1.05to 1.35, which may be the same or substantially the same as that for theprepared portion of zeolite X. However, zeolite X-precursors such askaolin clay often have lower Si/Al ratios, for example about 1.0, andtherefore normally do not convert to the desired, higher ratio zeoliteX.

However, it is possible to modify the procedure in which the zeoliteX-precursor is converted to zeolite X, in synthesis of abinder-converted composition, to increase the silica to alumina molarratio of the converted portion of zeolite X. This may be achievedthrough the addition of silica source such as colloidal silica sol,silicic acid, sodium silicate, silica gel, or reactive particulatesilica (e.g., diatomaceous earth, Hi—SiI, etc.). The silica source canbe added during the adsorbent particle forming step, to the causticdigestion step, or both. The amount of silica added is such that theoverall reaction mixture of zeolite X-precursor (e.g., meta-kaolin) andthe silica source is controlled such that the reaction composition fallsinto the following range: Na₂O/SiO₂=0.8-1.5, SiO₂/Al₂O₃=2.5-5,H₂O/Na₂O=25-60.

The use of a separate source of silica can therefore allow thepreparation of a binder-converted composition in which the Si/Al ratioof both the prepared and converted portions of zeolite X are closelymatched (e.g., are both within the range from 1.0 to 1.5, and normallyfrom about 1.05 to 1.35), thereby overcoming the drawbacks discussedabove with respect to the use of lower ratio zeolite X in the adsorptiveseparation of pX. Advantageously, the increase in the silica to aluminamolar ratio of the converted portion of zeolite X can also improve thehydrothermal stability of the resulting binder-converted composition.

The relative amounts of the first prepared and second converted portionsof zeolite X in the binder-converted composition may be varied.According to some embodiments, the amount of zeolite X-precursor used inthe preparation of the formed particle will be in the range from about5% to about 40% by weight, and preferably from about 10% to about 30% byweight. These ranges therefore also correspond to the amounts ofconverted zeolite X that is present in representative binder-convertedcompositions described herein.

Preferably, the binder material content, after conversion to the secondzeolite is in a range of from 0 to 3 wt %. In exemplary binder-convertedcompositions, non-zeolitic material is substantially absent (e.g., ispresent in the composition generally in an amount of less than about 2%by weight, typically less than 1% by weight, and often less than 0.5% byweight). The absence or substantial absence of non-zeolitic or amorphousmaterial may be confirmed by analysis of the binder-convertedcomposition using X-ray diffraction and/or high resolution scanningelectron microscopy (HR-SEM) to verify crystal structure. Macro- andmicro-pore structure and distribution may by characterized and confirmedusing mercury porosimetry or liquid oxygen adsorption.

Determining LTA Zeolite Content in Zeolite X by XRD

As discussed above, the present invention requires that the X zeolitehas a mean diameter not greater than 2.7 μm. Additionally, the presentinvention also requires a low LTA-containing X zeolite. The LTA zeolitelevel must either be non-detectable or otherwise have a relativeintensity not greater than 0.35, as determined by the XRD methoddescribed under the characterization examples below. As discussed morefully below, the relative intensity of the LTA zeolite (relative “LTAintensity”) of the sample is determined from the sum of the integratedareas under three LTA-type zeolite peaks with Miller indices of (2 0 0),(4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50° 2θ,relative to the sum of the same peaks for highly crystalline standardNaA zeolite.

Beyond these three peaks, there are other peaks present in a XRD scan ofLTA-type zeolite. However, these three peaks, with Miller indices of (20 0), (4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50°2θ, tend to have the least overlap or interference from othernon-LTA-type zeolite materials and still provide a significant totalintensity for the sum of three peak intensities from the Na-exchangedLTA zeolite scan. Furthermore, XRD characterization of the zeolite Xsample for its LTA zeolite content must be obtained using asodium-exchanged form of the zeolite X and the LTA zeolite referencematerial (i.e., NaA zeolite), respectively.

Accordingly, the relative LTA intensity is calculated as 100 times thequotient of

$\frac{a\mspace{14mu}{sample}\mspace{14mu}{LTA}\mspace{14mu}{XRD}\mspace{20mu}{intensity}\mspace{20mu}{for}\mspace{20mu}{the}\mspace{20mu}{zeolite}\mspace{20mu} X}{\begin{matrix}{a\mspace{20mu}{reference}\mspace{20mu}{XRD}\mspace{20mu}{intensity}\mspace{25mu}{for}\mspace{20mu} a\mspace{20mu}{LTA}\mspace{20mu}{zeolite}} \\{{reference}\mspace{20mu}{material}\mspace{20mu}{consisting}\mspace{20mu}{essentially}\mspace{20mu}{of}\mspace{20mu}{LTA}\mspace{20mu}{zeolite}}\end{matrix}}$wherein the sample LTA XRD intensity for the zeolite X is the sum of theintegrated areas under three LTA zeolite peaks with Miller indices of (20 0), (4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50° 2θand the reference XRD intensity for the LTA zeolite reference materialis the sum of the integrated areas under three LTA zeolite peaks withthe same Miller indices and related 2θ values.

As can be seen from FIG. 1, the reference material, a Na-exchangedzeolite A, (designated as scan A), provides the three LTA zeolite peakswith their respective Miller indices and 2θ values specified above,which can be used for determining the LTA zeolite content of differentsample materials such as, in this case, zeolite X. Scan B of acomparative material, prepared in accordance with the synthesis example(C-1) described below but fully Na-exchanged prior to XRD analysis,indicates the presence of detectable LTA zeolite in a zeolite X having amean diameter not greater than 2.7 μm, while Scan C of a low-LTAcontaining X zeolite indicates no detectable LTA zeolite, also fullyNa-exchanged prior to XRD analysis.

FIG. 2 illustrates the same comparative scans of FIG. 1, but with theNa-exchanged zeolite A reference scan not shown and at 10× magnificationso the three LTA zeolite peaks best indicating the presence of LTAzeolite, if any, are more easily observed.

For scan B, related to comparative example C-1, the integrated areasunder three LTA zeolite peaks with Miller indices of (2 0 0), (4 2 0),and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50° 2θ are 5.9, 2.3and 5.1. So the sum of these three specified peak areas is 13.3. Forscan A, related to the Na-exchanged zeolite A reference material, theintegrated areas under its peaks with Miller indices of (2 0 0), (4 20), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and 24.27±0.50° 2θ are 641.5,243.1 and 607.4. So, the sum of these three specified peak areas is1492. Accordingly, the relative LTA intensity for the sample is(13.3/1492)×100=0.89.

Ion-Exchange

The portions first prepared zeolite X and second converted zeolite X inthe binder-converted composition may be in their sodium form initially,and the sodium cations may be partially or wholly exchanged by differentcations, such as barium, potassium, strontium, and/or calcium, usingknown techniques. For example, the binder-converted composition,synthesized with zeolite X having at least some of its ion-exchangeablesites in sodium ion form, may be immersed in a barium ion containingsolution, or a barium and potassium ion containing solution, atconditions of time and temperature (e.g., about 0.5 to about 10 hours atabout 20 to about 125° C.) which can effect ion exchange or replacementof sodium ions with barium and/or potassium ions. Ion-exchange can alsobe conducted in a column operation according to known techniques, forexample by pumping preheated barium chloride/potassium chloridesolutions through a column of the adsorbent particles to completelydisplace the sodium cations of the zeolite X. Filtration of thebinder-converted composition, removal from the solution, andre-immersion in a fresh solution (e.g., having the same or differentratios or cations or other types of cations) can be repeated until adesired level of exchange, with the desired types and ratios of cations,is achieved.

Advantageously, the binder-converted composition will have at least 95%or substantially all (e.g., at least 99%) of the zeolite Xion-exchangeable sites exchanged with barium or a combination of bariumand potassium. Generally, no other metal ions occupy ion-exchangeablesites of the first prepared of zeolite X or the second converted portionof zeolite X in an amount effective to alter the adsorptive propertiesof the composition. In one embodiment, the zeolite X of thebinder-converted composition will have from about 60% to about 100% ofits ion-exchangeable sites exchanged with barium and from about 0% toabout 40% of its ion-exchangeable sites exchanged with potassium.

The number of ion-exchangeable sites decreases as the overall Si/AImolar ratio of the zeolite X increases. The overall ratio may beaffected by varying the ratio of either or both of the first preparedzeolite X and second converted zeolite X portions. Also, the totalnumber of cations per unit cell decreases as monovalent cations (e.g.,K+) are replaced by divalent cations (e.g., Ba⁺²). Within the zeolite Xcrystal structure, there exist many ion-exchangeable site locations,some of these being in positions outside of the supercages. Overall, thenumber and locations of cations in the zeolite crystal structure willdepend upon the sizes and numbers of the cations present, as well as theSi/Al molar ratio of the zeolite.

Para-Xylene Separation

Separation of pX is carried out by contacting a mixture of pX and atleast one other C₈ alkylaromatic hydrocarbon with an adsorbent. Forexample, a feed stream comprising the mixture of C₈ alkylaromatichydrocarbons may be contacted with a bed of the adsorbent in order toselectively adsorb, in an adsorbed phase, the pX, in preference toortho-xylene (oX), meta-xylene (mX), and ethylbenzene (EB). These otherC₈ alkylaromatic components of the feed stream may selectively passthrough the adsorption zone as a non-adsorbed phase.

Feed streams comprising mixtures of C₈ alkylaromatic hydrocarbons can beseparated from various refinery process streams (e.g., reformate) andmay also contain other compounds, such as C₉ alkylaromatic hydrocarbons.In one type of separation process, after the adsorptive capacity of theadsorbent is reached, the feed stream inlet flow to the adsorbent isstopped, and the adsorption zone is then flushed to remove anon-adsorbed phase, initially surrounding the adsorbent, from contactwith the adsorbent. The adsorbed phase, enriched in the desired pX, maybe thereafter desorbed from the adsorbent pores by treating theadsorbent with a desorbent, normally comprising a cyclic hydrocarbon(e.g., an aromatic ring-containing hydrocarbon) such as toluene,benzene, indan, para-diethylbenzene, 1,4-diisopropylbenzene, or mixturesthereof. The same desorbent is commonly used for both (i) flushing thenon-adsorbed phase into a raffinate stream comprising the desorbent and(ii) desorbing the adsorbed phase into an extract stream, alsocomprising the desorbent. Because the extract stream contains theadsorbed phase, which is enriched in pX, the extract stream will also beenriched in pX, relative to the feed stream, when considered on adesorbent-free basis.

The capacity of the adsorbent for adsorbing a specific volume of pX froma mixture of C₈ alkylaromatics, such as a mixture of xylenes (oX, mX andpX) and EB is an important characteristic, as increased capacity makesit possible to reduce the amount of adsorbent needed to separate the pXfor a particular charge rate of feed. So increased adsorbent capacityfor pX can result in a more efficient separation process provided goodinitial capacity for the extract component (pX in this case), as well astotal adsorbent capacity, should be maintained during actual use in anadsorptive separation process over some economically desirable life.

The rate of exchange of pX with the desorbent can generally becharacterized by the width of the peak envelopes at half intensityobtained from plotting the composition of various species in theadsorption zone effluent obtained during a pulse test versus time. Thenarrower the peak width, the faster the desorption rate. The desorptionrate can also be characterized by the distance between the center of thetracer peak envelope and the disappearance of an extract component whichhas just been desorbed. This distance is time dependent and thus ameasure of the volume of desorbent used during this time interval. Thetracer is normally a relatively non-adsorbed compound which movesthrough an adsorbent column faster than the materials to be separated.

Selectivity (β), for pX with respect to a raffinate component may becharacterized by the ratio of the distance between the center of the pXpeak envelope and the tracer peak envelope (or other reference point) tothe corresponding distance between the center of the raffinate componentpeak envelope and the tracer peak envelope (or reference point). Theselectivity corresponds to the ratio of the two components in theadsorbed phase divided by the ratio of the same two components in thenon-adsorbed phase at equilibrium conditions.

Selectivity may therefore be calculated from:Selectivity=(vol-% CA/vol-% DA)/(vol-% CU/vol-% DU)where C and D are two components of the feed mixture represented inweight percent and the subscripts A and U represent the adsorbed andnon-adsorbed phases, respectively. The equilibrium conditions aredetermined when the feed passing over a bed of adsorbent does not changecomposition, in other words, when there is no net transfer of materialoccurring between the non-adsorbed and adsorbed phases. In the equationabove, a selectivity larger than 1.0 indicates preferential adsorptionof component C within the adsorbent. Conversely, a selectivity less than1.0 would indicate that component D is preferentially adsorbed leavingan non-adsorbed phase richer in component C and an adsorbed phase richerin component D.

For a selectivity of two components approaching 1.0, there is nopreferential adsorption of one component by the adsorbent with respectto the other (i.e., they are both adsorbed to about the same degree withrespect to each other). As selectivity deviates from 1.0, there is anincreasingly preferential adsorption by the adsorbent for one componentwith respect to the other. Selectivity can be expressed not only for onefeed stream compound relative to another (e.g., pX to mX selectivity)but can also be expressed between any feed stream compound and thedesorbent (e.g., pX to para-diethylbenzene selectivity).

While separation of an extract component from a raffinate component istheoretically possible when the adsorbent selectivity for pX withrespect to the raffinate component is only slightly greater than 1, itis preferred that this selectivity is at least 2 for process economicconsiderations. Generally, the higher the selectivity, the easier theadsorptive separation is to perform. Higher selectivities allow use ofsmaller amounts of adsorbent to obtain the same productivity (e.g., pXrecovery) with an adsorbent having comparatively lower selectivity forthe same component in mixture (e.g., pX from oX, mX and EB).

The desorbent for an adsorptive separation process must be judiciouslyselected to satisfy several criteria. The desorbent should ideally havesufficient strength (i.e., be adsorbed strongly enough) to displace pXfrom the adsorbent at a reasonable mass flow rate, without being sostrongly adsorbed as to prevent pX from displacing the desorbent in afollowing adsorption cycle. In terms of the selectivity, it is preferredthat the adsorbent be more selective for the pX with respect to araffinate component than it is for the desorbent with respect to theraffinate component.

A performance parameter to be considered for the desorbent is thereforeits rate of exchange for pX in the feed or, in other words, the relativerate of desorption of pX. This parameter relates directly to the amountof desorbent that must be used in an adsorptive separation process todesorb pX from the adsorbent. Faster rates of exchange reduce the amountof desorbent needed and therefore improve operating efficiency withlarger desorbent-containing process streams, including the separationand recycle of desorbent from these streams. A desorbent selectivity of1 or slightly lower with respect to an extract component helps ensurethat all the pX is desorbed with a reasonable flow rate of desorbent,and also that extract components can displace desorbent in a subsequentadsorption step. One way of measuring selectivity can be by a “pulsetest” described below.

EXAMPLES

The present invention is described in further detail in connection withthe following examples which illustrate or simulate various aspectsinvolved in the practice of the invention. It is to be understood thatall changes that come within the spirit of the invention are desired tobe protected and thus the invention is not to be construed as limited bythese examples.

SYNTHESIS EXAMPLES Example S-1 Seed Crystals

An aluminate solution is prepared by mixing 755 g sodium hydroxide (50%NaOH), 425 g alumina trihydrate and 320 g water. The mixture is heatedto 230° F. and held for 15 minutes, then cooled to 120° F.

225 g aluminate solution is mixed with 1035 g water, 643 g sodiumhydroxide (50% NaOH) and 1298 g sodium silicate. After mixing, the batchis allowed to age for 72 hours to produce zeolite seed crystals.

Example S-2 Zeolite X

An aluminate solution is prepared by mixing 970 g sodium hydroxide (50%NaOH), 313 g alumina trihydrate and 418 g water. The mixture is heatedto 230° F.

559 g aluminate solution is mixed with 0.35 g seed crystals preparedaccording to Example S-1, 1744 g water, and 439 g sodium silicate.

The solution is then aged for 3.5 hours. The resulting crystals arefiltered from the solution and dried. The crystals are analyzed by XRDand ICP and determined to be zeolite X with a Si/Al framework molarratio of 1.275. The particle size is determined to be 1.7 μm bysedigraph analysis, according to the method described below.

Example S-3 Binder-Converted Zeolite X Composition

A 860 g portion of the zeolite X prepared according to Example S-2 isagglomerated with 140 g kaolin (ASP ⁴⁰⁰™ obtained from BASF), 20 gcornstarch and 20 g carboxymethyl cellulose (obtained from BASF) anappropriate amount of water. The mixture is extruded and the extrudatesare dried and activated at 650° C. for 4 hours under dry air. Theextrudates are then meshed to an average size of 0.5 mm.

A 100 g portion of the agglomerates is then immersed in 580 g of NaOHsolution with a concentration of 2.4% for binder conversion. The binderconversion temperature is 80-100° C. and lasts for 6 hrs.

COMPARATIVE EXAMPLES Example C-1 Comparative Zeolite X

Comparative zeolite X is prepared according to Example S-2, but using825 g sodium silicate and 0.7 g seed crystals prepared according toExample S-1.

The crystals are analyzed by XRD and ICP and determined to be zeolite Xwith a Si/Al framework molar ratio of 1.225. The particle size isdetermined to be 1.7 μm by sedigraph analysis, according to the methoddescribed below.

Example C-2 Comparative Zeolite X

Another comparative zeolite X is prepared by first forming an aluminatesolution by mixing 1058 g liquid sodium aluminate, 160 g sodiumhydroxide (50% NaOH) and 432 g water. Then, 523 g aluminate solution ismixed with 454 g water and 451 g sodium silicate.

The solution is aged for 2.3 hours and then crystallized for 5 hours.The crystals are filtered. The crystals are analyzed by XRD and ICP anddetermined to be zeolite X with a Si/Al framework molar ratio of 1.25.The particle size is determined to be 3.8 μm by sedigraph analysis,according to the method described below.

POST-SYNTHESIS TREATMENT EXAMPLES Example T-1

A sample prepared according to Example S-3 is ion-exchanged with amixture of 12 wt % BaCl and 1 wt % KCl solution. The ion-exchangesolution to solid ratio by mass is 21 to 1. The ion-exchange is carriedout in a column at 95° C. for 2 hours. After ion-exchange is completed,the column is drained and the solid material is then washed with wateruntil the chloride level is below 0.05 wt %. The washed sample is thendried in a Blue M oven at 250° C. under dry air flow for 1 hour. Thematerial obtained has an LOI of 5.7-5.8 wt %.

The water content of the adsorbent is expressed herein in terms of therecognized LOI test at 900° C. The LOI test is described in UOP TestMethod No. UOP954-03 (available through ASTM International, 100 BarrHarbor Drive, PO Box C700, West Conshohocken, Pa., 19428-2959 USA).

Example T-2

A comparative sample prepared according to Example C-1 is ion-exchangedin the same manner as Example T-1.

CHARACTERIZATION EXAMPLES Example CH-1 X-Ray Diffraction (XRD) forDetermining Relative Amount of LTA Zeolite

The relative amount of LTA zeolite in the zeolite of this invention canbe determined by XRD analysis. The x-ray patterns presented in thefollowing examples were obtained using standard XRD techniques.

The sample is ground to a powder (typically 150 mesh or less), thenplaced in a 53% relative humidity chamber containing a saturatedsolution of CaNO₃ at least overnight (˜15 hours). An approximately 1gram sample of the equilibrated powder is spread onto a XRD sampleholder and placed into the XRD instrument and scanned using parametersof 5.0° to 25.0° 2θ with a 0.02° step size and 10 second per stepcounting time. The XRD instrument is a Scintag XDS2000 instrument orfunctional equivalent equipped with a copper x-ray tube. The XRDinstrument is run at settings of 45 kV and 35 mA. The humidity in theinstrument is maintained at 53% humidity.

The relative amount of LTA zeolite in the sample is determined from thesum of the integrated areas under the three LTA zeolite peaks withMiller indices of (2 0 0), (4 2 0), and (6 2 2) at 7.27±0.16°,16.29±0.34° and 24.27±0.50° 2θ, relative to the sum of the same peaksfor highly crystalline standard NaA zeolite. The Miller indices, (h kl), designate which LTA-type zeolite peaks are to be included in theintegration procedure and are related to the peak positions by theequationλ=(2 a _(NaLTA) sin(θ_(hkl)))/(h ² +k ² +l ²)^(1/2)where λ is the x-ray wavelength (1.54059 Å for CuKα radiation),a_(NaLTA) is the NaA zeolite lattice parameter of 23.8 to 24.8 Ådepending on Si/Al ratio, and θ_(hkl) is one-half the diffraction anglefor the peak with Miller indices, (h k l).

Example CH-2 Sedigraph Analysis

Zeolite particle size is measured by a Micromeritics Sedigraph 5120Particle Size Analysis System. The Sedigraph 5120 is completelyautomatic and the operation of this unit is in accordance with theOperators Manual provided.

A zeolite sample is first dispersed in deionized water (2.8 gram ofzeolite/50 gram of D.I. water). The sample is then transferred to theSedigraph unit. From this equipment, the particle size distribution ofzeolite particles is obtained on a weight average basis. For example, aD50 or a D90 of the particle size distribution can be obtained. D50indicates a diameter for which 50 wt. % of the particles are below thespecified diameter, while D90 indicates a diameter for which 90 wt. % ofthe particles are below the specified diameter. Accordingly, D50 is alsoknown as the mean diameter.

Example CH-3 Pulse Test for Selectivity Performance

A “pulse test” is used to test adsorptive capacity, selectivity,resolution, and exchange rate. The pulse test apparatus includes atubular adsorbent chamber of approximately 70 cubic centimeters (cc) involume and having inlet and outlet portions at opposite ends of thechamber. The chamber is equipped to allow operation at constant,predetermined temperature and pressure. Quantitative and qualitativeanalytical equipment such as refractometers, polarimeters andchromatographs can be attached to an outlet line of the chamber and usedto detect quantitatively and/or determine qualitatively one or morecomponents in the effluent stream leaving the adsorbent chamber.

During a pulse test, the adsorbent is first filled to equilibrium with aparticular desorbent by passing the desorbent through the adsorbentchamber. A small volume or pulse of the feed mixture, which may bediluted with desorbent, is injected by switching the desorbent flow tothe feed sample loop at time zero. Desorbent flow is resumed, and thefeed mixture components are eluted as in a liquid-solid chromatographicoperation. The effluent can be analyzed on-stream or, alternatively,effluent samples can be collected periodically and analyzed separately(off-line) and traces of the envelopes of corresponding component peaksplotted in terms of component concentration versus quantity of effluent.

Information derived from the pulse test can be used to determineadsorbent void volume, retention volume for pX or a raffinate component,selectivity for one component with respect to the other, stage time, theresolution between the components, and the rate of desorption of pX bythe desorbent. The retention volume of pX or a raffinate component maybe determined from the distance between the center of the peak envelopeof pX or a raffinate component and the peak envelope of a tracercomponent or some other known reference point. It is expressed in termsof the volume in cubic centimeters of desorbent pumped during the timeinterval corresponding to the distance between the peak envelopes.

A sample prepared according to Example S-3 and ion-exchanged accordingto Example T-1 is evaluated in the adsorptive separation of pX. Acomparative sample prepared according to Example C-1 and ion-exchangedaccording to Example T-2 is also evaluated.

A standard pulse test as described above was performed by first loadingthe adsorbent in a 70 cm³ column under the desorbent para-diethylbenzene(pDEB). A feed pulse containing equal quantities of EB and each of thethree xylene isomers, together with a normal nonane (n-C₉) tracer, isinjected. Pulse tests are performed at various column temperatures inthe range from 121° C. to 177° C. (250° F. to 350° F.) to examine theeffect of temperature on selectivity. The pX selectivities weredetermined from the component peaks obtained from each of these pulsetests, and the results at 150° C. are shown in Table CH-1 below.

Example CH-4 Capacity Testing

A sample prepared according to Example S-3 and ion-exchanged accordingto Example T-1 is evaluated for its capacity in the adsorptiveseparation of pX. A comparative sample prepared according to Example C-1and ion-exchanged according to Example T-2 is also evaluated.

A column containing 70 cm³ of the adsorbent, initially loaded underpDEB, is charged with a sample feed mixture containing oX, mX, pX, andEB. Breakthrough tests are performed at a column temperature of 150° C.to determine the adsorbent's capacity (cm³) and pX/pDEB selectivity (asdefined above) at LOI=5.7-5.8%, and the results are shown in Table CH-1below.

TABLE CH-1 Capacity Sample P/E P/M P/O (cm³) pX/pDEB F D/F S-3/T-1 1.85.4 4.8 12.5 1.24 101 0.97 C-1/T-2 1.8 5.4 5.0 12.0 1.39 100 1.06

Based on the selectivity and capacity results, simulated moving bed(SMB) modeling analysis is used to estimate the feed throughput anddesorbent to feed (D/F) requirement in a commercial pX separationprocess. The results comparison is also shown in Table CH-1. The feedrate increase of S-3/T-1 over C-1/T-2 is 1%, whereas the desorbentrequirement is reduced to 92%. This represents significant reduction inthe amount of desorbent required to efficiently operate a pX separationprocess. D/F is based on mass flow ratio. Here we assume C-1/T-2 case isthe base case at 100.

The invention claimed is:
 1. A process for the separation of para-xylenefrom a mixture of C₈ alkylaromatics, comprising contacting the mixtureof C₈ alkylaromatics with a zeolitic binder-converted composition underadsorption conditions, the zeolitic binder-converted compositioncomprising: a. a zeolite X composition having at least a first zeolite Xhaving a mean diameter not greater than 2.7 microns, as determined bysedigraph analysis, and a second zeolite X, wherein the second zeolite Xis obtained by converting a binder material to the second zeolite X andthe binder material is in a range from 5 to 30 wt % of the zeolite Xcomposition, and b. an unconverted binder material content, afterconversion to the second zeolite X is complete, in a range from 0 to 3wt % of the zeolite X composition; wherein the zeolite X composition hasi. an average Si/Al framework mole ratio in a range from 1.0 to 1.5,wherein the Si/Al framework mole ratio of the first zeolite and thesecond zeolite may be the same or different; and ii. a relative LTAintensity not greater than 1.0, as determined by a x-ray diffraction(XRD) method using a source of CuKα radiation to obtain XRD intensitiesin range from 5° to 25° 2θ, wherein, the relative LTA intensity iscalculated as 100 times the quotient of$\frac{a\mspace{14mu}{sample}\mspace{14mu}{LTA}\mspace{14mu}{XRD}\mspace{20mu}{intensity}\mspace{20mu}{for}\mspace{20mu}{the}\mspace{20mu}{zeolite}\mspace{20mu} X}{\begin{matrix}{a\mspace{20mu}{reference}\mspace{20mu}{XRD}\mspace{20mu}{intensity}\mspace{25mu}{for}\mspace{20mu} a\mspace{20mu}{LTA}\mspace{20mu}{zeolite}} \\{{reference}\mspace{20mu}{material}\mspace{20mu}{consisting}\mspace{20mu}{essentially}\mspace{20mu}{of}\mspace{20mu}{LTA}\mspace{20mu}{zeolite}}\end{matrix}}$ wherein,
 1. the sample LTA XRD intensity of the zeolite Xcomposition is the sum of the intensities for each LTA peak with Millerindices of (2 0 0), (4 2 0), and (6 2 2) at 7.27±0.16°, 16.29±0.34° and24.27±0.50° 2θ, and
 2. the reference XRD intensity of the LTA-typezeolite reference material is the sum of the intensities for each LTApeak with Miller indices of (2 0 0), (4 2 0), and (6 2 2) at 7.27±0.16°,16.29±0.34° and 24.27±0.50° 2θ, wherein,  the sample LTA XRD intensityand the reference XRD intensity are each  a. obtained for asodium-exchanged form of the zeolite X composition and the LTA-typezeolite reference material, respectively, and  b. equilibrated at 50%relative humidity.
 2. The process of claim 1 wherein the unconvertedbinder material content, after conversion to the second zeolite X iscomplete, is in a range from 0 to 2 wt % of the zeolite X composition.3. The process of claim 1 wherein the average unit cell size of thezeolite X composition is in a range from 24.99 Å to 24.95 angstroms, asdetermined by XRD of a Na-exchanged form of the zeolite X compositionequilibrated at 50% relative humidity.
 4. The process of claim 1 whereinthe average unit cell size of the zeolite X composition is in a rangefrom 24.985 Å to 24.955 angstroms, as determined by XRD of aNa-exchanged form of the zeolite X composition equilibrated at 50%relative humidity.
 5. The process of claim 1 wherein the average Si/Alframework mole ratio of the zeolite X composition is in a range from1.15 to 1.35.
 6. The process of claim 1 wherein the LTA intensity of thezeolite X composition is not greater than 0.8.
 7. The process of claim 1wherein the zeolite X is ion-exchanged with barium, potassium, andcombinations thereof.
 8. The process of claim 7 wherein the contactingstep is conducted in a simulated moving bed apparatus.
 9. The process ofclaim 8 wherein para-diethylbenzene is used to desorb the para-xylenefrom the zeolitic binder-converted composition and wherein thepara-xylene to para-diethylbenzene selectivity is in a range from 1.15to 1.35 at LOI=5.7-5.8%.
 10. The process of claim 8 wherein the zeoliticbinder-converted composition has an adsorbent capacity of at least 12.5cm³ at LOI=5.7-5.8%, as determined at 150° C. for 70 cm³ of the zeoliticbinder-composition.